Distillation using mechanical advantage through mulitiple expanders

ABSTRACT

An energy-saving method and system for distilling, desalinating or purifying water relating to a method of increasing the amount of heat recycled back into the system. The system involves powering a compressor using a series of expanders and the energy derived from each expander cumulatively powers the compressor. The compressor draws vapor from seawater contained in an evaporator and compresses it into a condenser. The heat given off by the condenser is absorbed by the evaporator and recycled back into the system.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application claims priority to U.S. Pat. No. 10,233,094 filed Dec.5, 2014 and U.S. Non-Provisional Ser. No. 15/230,295 filed on Aug. 5,2016, and the respective disclosures are incorporated herein byreference to the extent that they do not conflict with the presentapplication.

BACKGROUND OF THE INVENTION 1. Field of the Invention

The present invention relates generally to distillation systems andmethods, and particularly to a low cost, energy-saving method and systemfor distilling, desalinating or purifying water and illustrates relatesto a method of increasing the amount recycled heat back into the systemas well as a more simplified and effective system than that known in thepresent industry.

2. Description of the Related Art

Distillation is well known process and involves heating a liquid untilit boils into a gas-phase, then condensing the gas back into aliquid-phase and collecting the condensed gas. The heating of the liquidinvolves high energy consumption, which makes the distillation processexpensive. What is needed is a new and improved distillation method andsystem that achieve the same results with a considerably less amount ofenergy.

The aspects or the problems and the associated solutions presented inthis section could be or could have been pursued; they are notnecessarily approaches that have been previously conceived or pursued.Therefore, unless otherwise indicated, it should not be assumed that anyof the approaches presented in this section qualify as prior art merelyby virtue of their presence in this section of the application.

BRIEF INVENTION SUMMARY

This Summary is provided to introduce a selection of concepts in asimplified form that are further described below in the DetailedDescription. This Summary is not intended to identify key aspects oressential aspects of the claimed subject matter. Moreover, this Summaryis not intended for use as an aid in determining the scope of theclaimed subject matter.

In one exemplary embodiment, the system to distill seawater with acondensing probe and recycled heat includes a compressor that is poweredby an external motor or by energy derived from an expansion system. Thecompressor draws in water vapor from the boiling seawater contained inan evaporator and compresses the vapor to an elevated temperature into acondenser where it condenses into pure water. In this example, it isassumed that the starting temperature of the seawater in the evaporatoris preheated to 212° F. and the steam from the evaporator is compressedto a temperature of 222° F.

In another exemplary embodiment, the system to distill seawater with acondensing probe and recycled heat recycles the heat in the distillationprocess and reuses the heat to run the distillation process again,creating an energy loop. To help achieve this process, the condenser isplaced within the evaporator so that the heat given off by the condenseris absorbed by the boiling seawater in the evaporator. This isparticularly important, in that the latent heat of condensation isabsorbed by the latent heat of vaporization. The reabsorption of thelatent heat back into the system greatly reduces the amount of externalenergy required to operate the distillation process. The latent heat ofvaporization comprises the greatest portion of heat required to operatethe distillation process. As an example, the latent heat of vaporizationof water at 100 degrees ° C. is approximately 540 cal./gm. However, ifthis heat is recycled it would greatly decrease the amount of energyrequired to run the process.

In another exemplary embodiment the system to distill seawater with acondensing probe and recycled heat utilizes at a given pressure,seawater that boils at a slightly higher temperature than pure water.For example, at atmospheric pressure, pure water boils at 100 C andseawater boils at 102 C. For this reason the vapor emitted from theevaporator containing the boiling seawater is compressed to a highertemperature so that the water vapor may be directed back into the coolerevaporator and condensed. In this process, heat is returned and recycledback to the evaporator. In discussing the following embodiments and forsimplification, it is assumed that distilled water and seawater have thesame boiling point and the latent heat of vaporization is the same at agiven temperature and pressure.

The above embodiments and advantages, as well as other embodiments andadvantages, will become apparent from the ensuing description andaccompanying drawings.

BRIEF DESCRIPTION OF THE DRAWINGS

For exemplification purposes, and not for limitation purposes, aspects,embodiments or examples of the invention are illustrated in the figuresof the accompanying drawings, in which:

FIG. 1 illustrates a diagram of a distillation system, according to anaspect.

FIG. 2 illustrates a diagram of a countercurrent heat exchange system,according to an aspect.

FIG. 3 illustrates a diagram of a distillation system having anexpansive section as a source of energy to power the distillationsystem, according to an aspect.

FIG. 4 illustrates a diagram of a distillation system having anexpansive section as a source of energy to power the distillation systemand a more elaborate condenser with an increased surface area, accordingto an aspect.

FIG. 5A illustrates a partial diagram of a distillation system having anevaporator with a plurality of vertical blades, according to an aspect.

FIG. 5B illustrates a partial diagram of a distillation system having anevaporator with a plurality of horizontal blades, according to anaspect.

FIG. 6 illustrates a one way heat system, according to an aspect.

FIG. 7 illustrates a diagram of a distillation system with a mechanicaladvantage, wherein an expander displaces a greater volume of water vaporthan the compressor connected to the expander, according to an aspect.

FIG. 8 illustrates a diagram of a distillation system having a chemicalmechanical advantage system, according to an aspect.

FIG. 9 illustrates a diagram of a distillation system in which excessvapor expelled from condenser 410 is directed to a condenser and into anevaporator, according to an aspect.

FIG. 10 illustrates a diagram of a distillation system having a countercurrent heat exchange system that transfers heat through latent heat,according to an aspect

FIG. 11 illustrates a diagram of a distillation system utilizing acombination of the stepped up system using chemical mechanicaladvantage, and a counter current latent heat exchange system, accordingto an aspect.

FIG. 12 illustrates a diagram of a distillation system having cells,wherein each cell contains its own evaporator, condenser and expander,and, also has incorporated the counter current latent heat exchangesystem, according to an aspect.

FIG. 13 illustrates a diagram of a distillation system having a countercurrent latent heat exchange system using solely water, according to anaspect.

FIG. 14 illustrates a diagram of a distillation system having aplurality of expanders interconnected and contributing energy to power acompressor, and, also has incorporated a conduit transporting brine froman evaporator and recycling its heat back into the system, according toan aspect

FIG. 15. illustrates vapor from an evaporator being compressed by acompressor and directly transported through a series of evaporators.

FIG. 16 illustrates a diagram of an energy producing system having aplurality of expanders interconnected and contributing energy to power agenerator.

DETAILED DESCRIPTION

What follows is a description of various aspects, embodiments and/orexamples in which the invention may be practiced. Reference will be madeto the attached drawings, and the information included in the drawingsis part of this detailed description. The aspects, embodiments and/orexamples described herein are presented for exemplification purposes,and not for limitation purposes. It should be understood that structuraland/or logical modifications could be made by someone of ordinary skillsin the art without departing from the scope of the invention. Therefore,the scope of the invention is defined by the accompanying claims andtheir equivalents.

FIG. 1 illustrates a diagram of a distillation system, according to anembodiment. As shown, the distillation system 100 having a condenser 135immersed within the seawater 126 contained in evaporator 130 and inaddition may have a condensing probe 140, an extension of condenser 135,that may be encircled by an outer pipe 153 containing incoming seawater152, such that heat is transferred from the condensing probe 140 intothe encircled seawater 152. Preferably, the condensing probe 140 isconfigured to increase the surface area and duration that heat istransferred from the high temperature steam 137 onto the incomingseawater 152. To this end, the condensing probe 140 depicted in FIG. 1and described herein is only an example. Various other configurationsmay be adopted. For example, a plurality of probes may be utilized toincrease further the surface area and thus increase heat transfer. It isadvantageous to insert the condensing probe 140 deep into the encirclingseawater to insure early contact with the cool incoming seawater. Inthis regard the incoming seawater begins to absorb heat early on and bythe time it reaches the evaporator 130, enough heat should have beenabsorbed and its temperature should have gradually risen to the level ofthe temperature of the seawater 126 boiling in the evaporator 130. Aheat source 105, 305 may be applied to the incoming seawater 152, asnecessary, to any point prior to reaching the area of the condensingprobe 140 to ensure the seawater reaches the desired temperature as itenters the evaporator 130.

The highest temperature level of the seawater is in the evaporator 130and the lowest temperature level is at the holding reservoir (FIG. 2,230) as it enters the system. Hence the greatest rate of condensationwithin the condensing probe 140 occurs when the steam 137 initiallycomes in contact with the cool incoming seawater 152 and slowest rate ofcondensation occurs when the condensing probe 140 approximates theevaporator 130.

To some extent the early onset of condensation within the condensingprobe 140 at the cooler regions of the incoming seawater help decreasethe pressure level within the condensing probe 140 and hence the workrequired by the compressor 120 to compress the vapor 136 from theevaporator 130 into the condenser 135. Since a portion of the steam 137has condensed at the cooler regions of the incoming seawater, it has asuction effect on the vapor entering the condensing probe 140 from thecompressor 120.

A form of circulation occurs as the incoming seawater 152 boils at theouter surface of the condensing probe 140 and bubbles ascend into theevaporator 130. This improves heat exchange and helps speed up thedistillation rate.

Insulation may be applied to the distal portion and the tip 142 of thecondensing probe 140, as necessary, to slow down and regulate the rateof heat transfer and avoid extreme temperature differentials between thehigh temperature of the steam 137 within the condensing probe 140 andthe cool temperature of the incoming seawater 152, to prevent crackingor damage to the condensing probe 140 due to the extreme temperaturedifferences.

A flow regulator 150 may be placed near the end of the outflow of thecondensed water 154 to regulate the amount of steam 137 contained withinthe condensing probe 140 and the duration the steam 137 conducts heatinto the inflow of seawater 152, thus regulating the rate of heatexchange into the incoming seawater 152 to assure and regulate the timeduration for optimum heat transfer. Also, by regulating the outflow ofcondensed water 154, suitable pressure within the condensing probe 140is maintained avoiding the temperature of the steam to drop below thetemperature of the evaporator 130. If the pressure in the condensingprobe 140 is higher than atmospheric pressure, the condensed water 154should flow out as the flow regulator 150 releases.

Subsequent to the condensation of the steam 137, the outflow ofcondensed water 154 exiting the condensing probe 140 still containsusable heat capable of being recycled back to the system. A countercurrent heat exchange system 151 (FIG. 2, 200) may help recapture andrecycle this heat back into the distillation system 100.

As the condensed water 154 and seawater 152 flow in opposite directions,heat from the condensed hot water 154 is gradually given-off to thesurrounding incoming cooler seawater 152. Hence, the outflowingcondensed water 154 becomes cooler. Conversely the inflowing seawater152 becomes hotter as it absorbs heat and approaches the condensingprobe 140 and ultimately the evaporator 130.

The compressor 120 may be actuated by an external motor 110 or by othermeans as it will be explained hereinafter when referring to FIGS. 3-4for example. The compressor 120 draws in water vapor 136 from theboiling seawater contained in an evaporator 130 and compresses the vaporinto a condenser 135 and further into a condensing probe 140 as shown,where it condenses into pure water.

Thus, it should be apparent that an important aspect is to recycle theheat in the distillation process and reuse the heat to run thedistillation process again, creating an energy loop. To help achievethis process, the condenser 135 and/or the condensing probe 140 may beplaced completely or partially (as shown in FIG. 1) within theevaporator 130 so that the heat given off by the condenser 135 isabsorbed by the boiling seawater 126 in the evaporator. Any portions ofthe condenser 135 or condensing probe 140 not placed within theevaporator 130 or within a heat exchange system 151, would preferablyneed to be insulated such that to prevent heat loss by the distillationsystem 100. This is particularly important, in that this causes thelatent heat of condensation to be absorbed by the latent heat ofvaporization. The reabsorption of the latent heat back into the systemgreatly reduces the amount of external energy required to operate thedistillation process. The latent heat of vaporization comprises thegreatest portion of heat required to operate the distillation process.As an example, the latent heat of vaporization of water at 100 degreesC. is approximately 540 cal/gm. However, if this heat is recycled,rather than allowing the heat to escape into the environment, it wouldgreatly decrease the amount of energy required to run the distillationsystem.

For the purpose of this discussion, for simplification, we are assumingthat distilled water and seawater have the same boiling point and latentheat of vaporization at a given temperature and pressure. In thisexample, also for simplification, we are assuming that the startingtemperature of the seawater 126 in the evaporator 130 is preheated to212 Fahrenheit (F) and the steam 136 from the evaporator is compressedby compressor 120 to a temperature of 222 F. However, in-reality at agiven pressure, seawater boils at a slighter higher temperature thanpure water, (approximately 102 Celsius degree (216° F.) at sea level).For this reason, the steam 136 emitted from the evaporator 130containing the boiling seawater 126 is compressed into a highertemperature (222 F) so that the steam 137 may be, as explained earlier,passed through the cooler evaporator 130 and condensed. In this processheat is returned and recycled back to the evaporator.

It should be understood that, the starting temperature of the evaporator130, as well as any heat required to maintain its temperature due toheat loss of the system, may be provided by a heating source eitherthrough heating elements 106, solar energy or burning of fuels or othersuitable means.

The preceding example pertains to distilling seawater to obtain purewater. However, any liquid, for example liquid chemicals used inindustries, or unpurified water may be distilled using the system fromFIG. 1, including that of treatment facilities, brackish water, etc.

FIG. 2 illustrates a diagram of a counter current heat exchange system200.

A complete heat exchange is difficult if not impossible. However, thegoal is to come as close as possible to a complete heat exchange.

Toward the end of the outflow of the condensed water 220, thetemperature of the condensed water 220 is the lowest and the heatabsorption rate is the slowest. At this point, to optimize heatexchange, the condensed water 220 may be passed through coils orradiators, before it enters a condensed water holding tank 222.Furthermore, the outflowing condensed water 220 may be piped through andstored in container(s) 223 within the holding reservoir 230 containingthe inflowing seawater, so that the last bit of the heat from thecondensed water 220 is transferred to the sea water 210 therein. Thestorage containers 223 should be constructed of material that readilyconducts heat.

Theoretically, if the counter current heat exchange 200 is long enoughand insulated well to prevent heat loss, the condensed water 220 maygive off enough heat and its temperature may be reduced to be the sameor close to the temperature of the incoming seawater 210 and thetemperature of the incoming seawater 210 may absorb heat and itstemperature increased to be the same or close to the temperature of thecondensed water 220 leaving the condensing probe (FIG. 1, 140).

Expansive Section

FIG. 3 illustrates a diagram of a distillation system having anexpansive section as a source of energy to power the distillationsystem, replacing or augmenting motor 110, according to an embodiment.

An important aspect of the distillation system 300 of FIG. 3 is the useof a fluid 351A and 351B in which the fluid 351A and fluid 351B may be arefrigerant, R-410A for example. In this example, refrigerant R-410A,351A is in a gas phase and liquid phase mixture contained in anevaporator or a boiler 360, and may absorb heat from its surroundingscausing the refrigerant 351A to boil. The increase in the refrigerantvapor 351A in the boiler 360 causes an increase in pressure. Thepressurized refrigerant vapor 351A is preferably communicated from theboiler 360 through an expander 370 into condenser 380 where thegas-phase refrigerant 351A condenses into a liquid-phase 351B, resultingin a decrease in pressure in condenser 380. Heat may be expelled fromcondenser 380 into a cooler environment. The expander 370 is placedbetween the high pressure of the boiler 360 and the low pressure ofcondenser 380. The expander 370 is preferably actuated by the differencein pressure between the boiler 360 and condenser 380 and the energyderived from the expander 370 is transferred to and actuates thecompressor 304 of the compressive section 300B of the distillationsystem 300. The condensed liquid-phase refrigerant 351B is preferablypumped from condenser 380 back into the boiler 360 via a pump 390.

The portion of the system from which energy is derived, including theboiler 360, expander 370 and condenser 380 is termed the expansivesection 300A and the portion of the section in which the compressor 304compresses vapor, including the evaporator 306, compressor 304,condenser 307 and the condensing probe 308 are termed the compressivesection 300B.

An option for enhancing the vaporization of the liquid-phase refrigerant351B, as it enters the boiler 360, is to pump the liquid-phaserefrigerant 351B with sufficient force through an expansion valve 392creating a spray of the refrigerant 351B. The sudden drop in pressurecauses the refrigerant 351B droplets to vaporize more readily.

The heat source for the boiler 360 may preferably come from ambienttemperatures or may be fortified by, for example, solar energy such asfrom parabolic reflectors, reflective mirrors 362, solar panels or thelike.

As previously discussed, the heat source for the evaporator 306/130 forproviding the starting temperature and temperature maintenance of theseawater may be provided by a heating element 306A/106, solar energy,burning fuels or the like.

A pump 306B may be provided to increase the pressure of the incomingseawater into the evaporator 306 thus providing for higher boilingtemperatures of the seawater. As it will be discussed later, greateryields of distilled water are achieved when the temperature of theseawater in the evaporator is at higher levels. This is due to the vaporconcentration and saturation points becoming higher as the temperatureof the water vapor increases. Together, in association with thecompressor 304, the pump 306B and the outflow regulating valve 310regulate and maintain the pressure and temperature of the evaporator 306and the condensing probe 308. Pump 306B may also be used to increaseheat exchange by circulating the seawater about the condensing probe308. For example, a whirling motion of the seawater around thecondensing probe 308 may be created by the implementation of pump 306B,or the like, having a dual role and acting as an impeller to circulatethe seawater.

Another option of reutilizing heat is to divert a portion or all of theoutflow of the condensed water 220, through piping 361, into the boiler360 of the expansive section 300A. This is particularly useful at theend phase of the counter current heat exchange 200. At the end phase,the condensed water 220 is at a low temperature due to most of its heathaving been given-off. Additionally, at this point there is a slow rateof heat exchange. Provided the temperature of the condensed water 220,diverted into piping 361, is high enough to cause the refrigerant 351 Ato boil in the boiler 360, the low grade heat of the condensed water 220will be absorbed by the latent heat of the boiling refrigerant 351 A.The absorption of heat, in this manner, is at a much faster rate than itwould have been if the condensed water 220 would have ran its normalcourse and had exchanged its heat through ordinary conduction.Furthermore, the heat from the diverted condensed water 220 may beutilized by the boiler 360 as an energy source to help drive theexpander 370. A 3-way valve 320 may regulate the portion of thecondensed water 220 delivered to the boiler 360 of the expansive section300A of the system. As an option, heat from condenser 135/307 may alsobe diverted through piping 361 to boiler 360 in the form of steam beforeit becomes condensed in condensing probe 140/308 or may be diverted inthe form of condensed water 220 at any point along the counter currentheat exchange system 151. In the instance where steam is diverted toboiler 360, the steam becomes condensed in boiler 360. In each instancewhether the heat is derived from steam or condensed water, the heatgiven off is captured as an energy source by boiler 360 as refrigerant351A expands during boiling and help drive the expander 370. It is notedthat heat from condenser 307 either in form of steam 137 or condensedwater 220 may be diverted through piping 361 into boiler 360 andbypassing either the condensing probe 308 or counter current heatexchange system 200 or both.

Piped cool ocean water 381 may be utilized to condense the refrigerant351A in condenser 380 of the expansive section 300A of the system.Seawater of cooler temperatures may be obtained from the depths of theocean, thus providing a greater temperature differential between theboiler 360 and condenser 380 and in turn a greater force exerted on theexpander 370. As the piped ocean water 381 passes through condenser 380,heat is absorbed and transferred to the ocean water 381.

Yet another embodiment involving the recapturing of heat is to make useof the heated ocean water as it exits condenser 380. This embodimentincludes piping the cool seawater 381 through the chamber of condenser380. As refrigerant 351A vapor becomes condensed, heat is transferred tothe cool incoming piped seawater 380. As a result, the seawater 380becomes pre-warmed and then may be stored in a holding reservoir (FIG.2, 230) before it enters the counter current heat exchange system 200and subsequently into the evaporator 306 of the compressive section 300Bof the distillation system. The pre-warmed seawater may also enter theevaporator 306 directly bypassing the counter current heat exchangesystem 200.

FIG. 4 illustrates a diagram of a distillation system 400 having anexpansive section 400B as a source of energy to power the distillationsystem and a more elaborate condenser 410 having an increased surfacearea, according to an embodiment.

The evaporator 425 receives seawater 411 from the counter current heatexchange system 200 and at this point (when entering the evaporator 425)the temperature level of the seawater 426 contained in evaporator 425should be at or near the temperature of its boiling point. At this pointthe seawater 426 has initially reached its boiling point. However, theseawater 426 must still gain additional heat to overcome the latent heatrequirement in order for it to boil. Since latent heat requires thegreatest portion of heat in the distillation process, a condenser 410filled with steam having a temperature greater than that of the seawater426 from evaporator 426 as well as having an increased surface area isdesirable.

For the purpose of simplification, the heat recycling element 361, shownin FIG. 3, regarding diverting the piped condensed hot water 220 orsteam 137 from the counter current heat exchange system 200 has beenomitted from the drawing of FIG. 4. However, all of the embodiments andelements of FIG. 3 may be incorporated into FIG. 4.

A heating source or element 420 coupled to a circulating fan 420A,similar to that of a hair dryer, may be placed inside the chamberleading to the condenser 410 to heat the steam 437 of the condenser 410to assure the temperature of the steam 437 in the condenser 410 isadequately above the temperature of the evaporator 425. Less heat isrequired to heat the steam in the condenser 410 than it is to heat theliquid water in the evaporator 425. To raise the temperature of 1 Kg ofsteam by 1° C. requires half the amount of heat to raise the samequantity of liquid water by 1° C.

Additionally there may be times when the seawater 426 within evaporator425 may be heated by heating source 306A or heating incoming seawater220 by source 305 prior to entering evaporator 425 to increase ormaintain the temperature at a desired starting point or during timeswhen the process of recycling heat is insufficient or faulty.

FIG. 3 and FIG. 4 depict the expansive section 400B of the systemproducing the energy to drive the compressive section 400A of thesystem. However, the expansive section 400B of the system may beeliminated and instead driven by a motor 110 or the like, as illustratedin FIG. 1. Use of the expansive section 400B however, may increase theefficiency of the distillation system 400 (300 in FIG. 3) as it may bepowered by readily available heat energy in the environment (e.g., solarheat captured by solar panels, mirrors, or solar heat accumulated in theattic of houses, etc).

Additionally, on days when the sun is not strong enough to provide theboiler 360 with sufficient energy to fully drive the compressor 422,external energy may be applied to augment the work of the expander 370.The external energy may be in the form of a motor 110 (or other energysource), coupled to the expander 370 and/or the compressor 422. In theaugmentation configuration, the expander 370 may derive its energypartially from a solar source and the remaining portion from an externalaugmenting motor.

Example 1 is an illustration of a mechanical advantage system in whichthe fluid 351A, 351B is refrigerant R-410A and is being used in theexpansive section 400B to drive the compressive section 400A to distillwater. The boiler 360 contains a gas phase and liquid phase mixture ofthe refrigerant R-410 351A. Evaporator 425 contains seawater andcondenser 410 contains condensed or the resultant distilled water 440.For the purpose of this illustration, it is assumed that seawater andpure water have the same boiling points.

The following example assumes a starting temperature in the evaporator425 to be 212° F. and that all of the heat is circulated back into thesystem 400.

Example 1

Chart 1 lists the parameters to be applied to the systems illustrated inFIG. 3 or FIG. 4.

CHART 1 Water Condenser 410 Temperature 222° F. Pressure 18 PSI (denotedby P1) Evaporator 425 Temperature 212° F. Pressure 14.69 PSI (denoted byP2)

R-410A Boiler 360 Temperature 80° F. Pressure 236 PSI (denoted by P3)Condenser 380 Temperature 70° F. Pressure 201.5 PSI (denoted by P4)

-   -   Utilizing the parameters listed in Chart 1 and if A2=1 unit:        A1(P1−P2)=A2(P3−P4)  Equation 1:    -   Compressive Expansive        A1(18−14.69) PSI=A2(236−201.5) PSI.        (A1) 3.31 PSI=34.5 PSI        A1=10.42 sq·in.

Note: A1 and A2 is the area that partitions the difference in pressureacting upon compressor 422 and expander 370 respectively. At equilibriumthere is a mechanical advantage of 10.42. If the area of displacement isproportional to the volume of displacement, then for every cubic meterof R410-A vapor displaced by the expander 370, 10.42 cubic meters aredisplaced by the compressor 422.

If the compressor displaces 10.42 times the volume of the expander,then:P1V1=P2V2 or Work 1=Work 2Work 1 compresses and Work 2 expandsor 3.31 PSI (10.42 cubic meters)=34.5 PSI (1 cubic meter)34.5 PSI (cubic meter)=34.5 PSI (cubic meter)

If the temperature of evaporator 306/425 is 212° F. then the density ofsteam at this temperature is 0.590 Kg/cubic meter: There is a yield of:10.42 (0.590 Kg/cubic meter)=6.14 Kg of water for every cubic meter ofR410-A displaced by the expander 370.

A relatively small temperature difference of 10° F., between thetemperature of the ambient air and that of the ocean water, is requiredto operate the system. In this example, this temperature differencebetween the ambient air and the ocean water may be readily obtainednaturally from the environment.

However, if the parabolic reflector or reflective mirrors 362 or othersources were utilized to provide additional heat to the boiler 360, muchgreater yields may be produced.

For example, if the temperature of the boiler 360 was raised by 10° F.to a temperature of 90° F., utilizing similar calculations as thoseperformed in Example 1, a yield of 12.97 Kg of water for every cubicmeter of R410-A displaced by the expander 370 would be obtained.

Compared to the boiler being at 80° F., producing a yield of 6.14Kg/cubic meter, the boiler at 90° F. produces a yield of 12.97 Kg/cubicmeter. The yield has more than doubled. Alternatively, the option ofutilizing a motor 110 as shown in FIG. 1 or a combination of a motor 110and an expansive section 400B to operate the compressive section 400Amay be implemented.

Creating a Heat Loop

Assuming that most of the heat was recycled and there was minimal heatloss in the compressive section 400A of the system, the compressivesection 400A would be assumed to be a closed loop system. When theexpander 370 drives the compressor 422, energy is introduced into theclosed loop as the compressor 422 increases the temperature of the steam437 in the condenser 410. If the recycling mechanism was efficientenough, most of the heat would return back into the compressive section400A, including the heat that was introduced by the expander 370.Theoretically, the temperature of the evaporator 425 would eventuallyincrease and hence increase the temperature of the entire compressivesection 400A. This is taking into consideration that the energyintroduced by the expander 370 becomes incorporated into part of thetotal heat contained in the compressive section 400A.

If both the seawater 426 in the evaporator 425 and the condensed water220 was at a temperature of 212° F. and assumed to contained the sameamount of internal heat and that if all the heat was recycled back intothe loop, the only energy needed to run the process would be that ofraising the temperature level of the steam 436 from the evaporator 425just high enough so that the steam 437 may condense and give-off heatback to the cooler seawater 426 in the evaporator 425.

Insulation is of great importance in minimizing heat loss. An effectivemethod of insulation is that of encasing the components of thecompressive section 400A and creating a vacuum between the componentsand encasing. This would function much like that of a thermos.

All heat exchange elements may be comprised of coils, radiators, tubeconvolutions or the like to increase surface area for the purpose ofachieving optimum heat exchange.

The introduction of external energy, into the heat loop by pumping theinflow of seawater 210 to elevated pressures into the evaporator 306/425also becomes recycled. The pump 306B steps up the system by increasingthe pressure in the evaporator 306/425 and elevating the startingtemperature in which the seawater 426 boils (see FIG. 3). The expander370, driving the compressor 304/422, is now able to compress the steam436 from the stepped-up evaporator 425 into a proportionally higherpressure and temperature into the condenser 410/307/308. The steam 437within the condenser 410 is then able to transfer heat, at a highertemperature level, back into the evaporator 425, thus maintaining thestepped-up temperature of the evaporator 425. Heat, if required, may beapplied to the seawater in the evaporator 425 to maintain or stabilizethe system.

Salt Removal from the Evaporator

In order to preserve heat, the salt that becomes concentrated in theevaporator 425 may be expelled with the use of a second counter currentheat exchange system. However, in this second counter currentapplication the outgoing salt water 441 leaving evaporator 425 has muchmore salt concentrated than the incoming seawater 442. As the highsalt-concentrated water 426 of evaporator 425 is being replaced with theless-concentrated incoming seawater 442, the salt level of the saltwater 426 in evaporator 425 becomes less concentrated. Similarly, aspreviously illustrated in the counter current heat exchange system 200in FIG. 2, the outgoing salt water 441 may be encircled by the incomingseawater 442 and in the process the incoming seawater 442 absorbs theheat from the outgoing salt water 441, thereby recycling and preservingheat. Furthermore, the seawater 426 in evaporator 425 may be allowed toconcentrate to the point the concentrated salt precipitates out ofsolution and settles to the bottom. The precipitated salt may then bepumped out.

FIG. 5A illustrates a partial diagram of a distillation system having anevaporator with a plurality of vertical blades, according to anembodiment.

A series of vertical blades 510 may be placed across the lower portionof evaporator 500, allowing the precipitated salt to pass between thevertical blades 510 and settle onto a tray 512 located at the bottom500A of evaporator 500.

FIG. 5B illustrates a partial diagram of a distillation system having anevaporator with a plurality of horizontal blades, according to anembodiment.

When the tray 512 becomes filled with salt, the tray 512 is thencompartmentalized as the vertical blades 510 rotate horizontally andcreate a partition separating the tray 512 from the seawater 526contained in evaporator 500. Once compartmentalized, the tray 512 may beremoved from the bottom 500 A of evaporator 500 and emptied of itsprecipitated salt content. The empty tray 512 is then placed back intothe bottom of evaporator 500 and the horizontal blades 520 resume theirvertical position. The intake of seawater 511 is pumped to a higherlevel than the seawater 526 contained in evaporator 500 to avoid theback flow of the concentrated seawater 526.

Seawater containing higher concentrations of salt has higher boilingtemperatures. However, this is of less significance if the heat isrecycled and returned back through the loop. It is noted that theparticular parameters utilized in these examples are for illustrativepurposes, and an array of different parameters and types of refrigerantsmay be utilized that may produce similar or improved results.

Overview of the Process

The boiler 360 contains a gas phase and liquid phase mixture ofrefrigerant R-410A 351A and absorbs heat from any available sourceincluding ambient heat, sun panels or parabolic reflectors 362. In thisparticular illustration the temperature of the refrigerant R-410A (3511Ain the boiler 360) is 80° F. and pressure is 236 PSI. The refrigerantR-410A being utilized in this example is for illustrative purposes only,any other refrigerant or liquid may be utilized in its place.

Condenser 380 transforms gas-phase refrigerant 351A to liquid-phaserefrigerant 351B and gives-off heat to the cool incoming piped seawater381. The temperature in condenser 380 containing R-410A is 70° F. andthe pressure is 201 PSI.

Evaporator 425 contains seawater 426 to be distilled. The temperature ofthe seawater 426 in evaporator 425 is 212° F. and the pressure is 14.69PSI.

Condenser 410 is located within evaporator 425. The steam 437 incondenser 410 condenses into pure water 440 as it gives-off heat to theseawater 426 in evaporator 425. The temperature in condenser 410containing steam 437 is 222° F. and the pressure is 18 PSI.

The compressor 422 draws steam 436 from the seawater 426 contained inevaporator 425 and compresses it into condenser 410. The temperature ofthe seawater in evaporator 425 is 212° F. and the temperature of thesteam 437 in condenser 410 is 222° F. Condenser 410 is located withinevaporator 425, and concurrently, heat is reabsorbed from condenser 410back to the seawater 426 in evaporator 425. In this manner latent heatbecomes recycled as the latent heat is given-off from condenser 410 andabsorbed by the evaporator 425.

Example 2 is an illustration showing a decrease in the level ofmechanical advantage when water is utilized on the expansive section400B, instead of R410A. Taking for example the parameters of chart 1 andinstead of using R-410A on the expansive section 400B, R-410A isreplaced with water. All temperature parameters remain the same asdepicted in example 1 and listed in chart 1. However, both thecompressive section 400A and the expansive section 400B of the systemuse water.

Example 2 Use of Water as the Refrigerant

Chart 2 lists the parameters to be applied in the system illustrated inFIG. 3 and FIG. 4.

CHART 2 Water Condenser 410 Temperature 222° F. Pressure 18 PSI (denotedby P1) Evaporator 425 Temperature 212° F. Pressure 14.69 PSI (denoted byP2) Boiler 360 Temperature 80° F. Pressure .507 PSI (denoted by P3)Condenser 380 Temperature 70° F. Pressure .363 PSI (denoted by P4)

Utilizing the parameters listed in Chart 1 and if A21 unit:

Note: A is the area that partitions and interphases the difference ofpressure.A1(P1−P2)=A2(P3−P4)  Equation 2:

-   -   Compressive Expansive        A1 (18−14.69) PSI=A2 (0.507−0.363) PSI.        (A1)3.31 PSI=0.144 PSI        A1=0.043 in.

At equilibrium there is a mechanical advantage of 0.043.

For every cubic meter of water vapor displaced by the expander 370,0.043 cubic meters of water vapor are displaced by the compressor304/422.

If the compressor 304/422 displaces 0.043 times the volume of theexpander 370, then:P1V1=P2V2 or Work1=Work2

-   -   Work 1 compresses and Work 2 expands        or 3.31 PSI (0.043 cubic meters)=0.144 PSI (1 cubic meter)        0.144 PSI (cubic meter)=0.144 PSI (cubic meter)

If the temperature of the evaporator is 212° F. then the density ofsteam at this temperature is 0.590 Kg/cubic meter. There is a yield of0.043 (0.590 Kg/cubic meter)=0.025 Kg of water vapor for every cubicmeter of water vapor displaced by the expander 370.

However, when utilizing R410-A in the expansive section 400B, as inexample 1, it produces a much higher yield (6.14 Kg of water/cubicmeter) when compared to the yield utilizing water (0.025 Kg ofwater/cubic meter). Utilizing R410-A in the expansive section 400Bproduces (6.14 kg/0.025 Kg=245.6) or 245.6 times greater yields than ifwater were to be utilized in the expansive section 400B.

As illustrated above, utilizing water in the expansive section 400 ofthis system would be impractical given that the pressure differencebetween the boiler 360 and the condenser 380 yields a force of only0.144 PSI. The force acting upon the expander 370 is minimal and notsufficient to operate the system. In contrast when utilizing R410A inthe expansive section 400B of this system, the pressure between theboiler 360 and the condenser 380 yields a force of 34.5 PSI.

However, the system is not intended to preclude the use of water as arefrigerant, in that water may be the refrigerant of choice in someapplications. In a mechanical advantage system, utilizing two fluidshaving different vapor pressure properties at given parameters oftemperature to produce a mechanical advantage, will be termed achemically induced mechanical advantage. In contrast, a mechanicaladvantage is produced by a mechanical advantage system when the expander370 and the compressor 304/422 simultaneously displaced a differentvolume of fluid. In some applications, it is advantages to use amechanical advantage in combination with a chemically induced mechanicaladvantage to achieve a desired outcome.

Example 3

Example 3 illustrates that distillation systems produce greater yieldswith increased temperature of the seawater 426 in evaporator 306/425. Inthis example the temperature of the seawater 426 in evaporator 425 is281° F. and the temperature of the condenser 410 is 291° F. Chart 3lists the parameters to be applied in the system illustrated in FIG. 3and FIG. 4. The parameters for the expansive section 400B remain thesame as those listed in chart 1. The parameters for the compressivesection 400A have been increased. However, the condenser 410 andevaporator 425 on the compressive section 400A of both chart 1 and chart3 have a temperature difference of 10° F.

CHART 3 Water Condenser 410 Temperature 291° F. Pressure 58 PSI (denotedby P1) Evaporator 425 Temperature 281° F. Pressure 50 PSI (denoted byP2)

R-410A The Boiler 360 Temperature 80° F. Pressure 236 PSI (denoted byP3) Condenser 380 Temperature 70° F. Pressure 201.5 PSI (denoted by P4)

Utilizing the parameters listed in Chart 3 and if A2=1, then:A1(P1−P2)=A2(P3−P4)

-   -   Compressive Expansive        A1(58−50) PSI:=A2(236−201.5) PSI.  Equation 3:        (A1)8 PSI=34.5 PSI        A1=4.31 sq·in.

Note: A1 and A2 is the area that partitions the difference in pressurein the compressor 304/422 and expander 370 respectively. At equilibriuma mechanical advantage of 4.31 is produced.

If the area of displacement is proportional to the volume ofdisplacement, then for every cubic meter of R410-A vapor displaced bythe expander 370, 4.31 cubic meters are displaced by the compressor 304.If the temperature of the evaporator 306 is 281° F. then the density ofsteam at this temperature is 1.90 Kg/cubic meter:

When the temperature of the seawater 426 in evaporator 306/425 is at atemperature of 281° F., there is a yield of: 4.31 (1.90 Kg/cubicmeter)=8.19 Kg of water for every cubic meter of R410-A displaced by theexpander 370. This is a greater yield than that in example 1 producing ayield of 6.14 Kg/cubic, when the seawater 426 temperature of evaporator306/425 is at 212° F.

Example 4 Use of the Expander to Power the System

Example 4 reduces the volume displacement of the compressor 304,illustrated in example 1, by 20%. The compressor 304 initially having avolume displacement of 10.42 (Cubic meter) PSI, now has a reduced volumedisplacement of 10.42 (0.20)=8.33 (Cubic meter).

Using this new parameter in equation 1, the expansive section 300A ofthe system will over power the compressive section 300B of the systemand will have 6.9 (Cubic meter) PSI of available work to drive thecompressive section 300B. The derivation is as follows:P1V1=P2V2 or Work1=Work2Work 1=compressor and Work 2=expander8.33(3.31)=1(34.5)  Equation 427.57 (Cubic meter) PSI<34.5 (1 Cubic meter) PSI34.5 (1 Cubic meter) PSI−27.57 (1 Cubic meter) PSI=6.9 (Cubic meter)PSI.

The expander 370 has 6.9 (Cubic meter) PSI of surplus work available tooperate the compressor 304. The surplus work overcomes the friction ofcompressor 304, 422 and expander 370, and allow the system to run, standalone, or without the need of external augmented energy. The greater thesurplus energy the greater the power and speed to run compressor304,422.

The illustrations previously discussed are only examples and theprinciples may also apply to other applications and scenarios utilizingdifferent refrigerants, mechanical ratios, temperature and pressureparameters, etc.

Heat Containment System

FIG. 6 illustrates a heat containment system 600 for the expansivesection 600B of the distillation system.

Typically boilers that collect heat from sun radiation lose heat to theenvironment through conduction. This embodiment helps prevent such loss.Sun rays from parabolic reflectors or mirrors 612 or the like penetratethe encasement 614, heating the boiler 610 of the expansive section 600and causing the refrigerant 615 A to boil. Sun rays are electromagneticradiation carrying heat. And, since electromagnetic waves are notimpeded by a vacuum, heat may be transferred via radiation throughvacuum layer 616 and both encasements 614 and heat the refrigerant 615Aof boiler 610.

As radiant energy contacts the refrigerant 615A, its energy istransformed into kinetic energy and heats the refrigerant 615A. The heatin the form of kinetic energy contained in boiler 610 becomes trappedand unable to escape to the outside as the kinetic energy of the heatedrefrigerant 615 A molecules is unable to penetrate and pass the vacuumbarrier. The vacuum barrier 616 acts as a thermal insulator similar tothat of a thermos. In utilizing this system, radiation energy is allowedto enter boiler 610 but the transformed kinetic energy, from theradiation, is prevented from escaping outside boiler 610. The heatcontainment system helps prevents heat loss to outside the boiler 610and forces the energy to pass through expander 370 as useful work.

The encasement 614 may be composed of transparent materials, or othermaterials capable of allowing the penetration of radiation or sun rays.It is noted that some electromagnetic radiation may reflect and leavethe system.

The energy derived from the expansive section 600B, utilizing the oneway heat system 600 may be implemented as a power source to operate anyof the pre-mentioned compressive sections 100, 300B, 400A and 600A.

FIG. 6 illustrates the one way heat system 600 used in conjunction withan expander 370 of the expansive section 600B. The energy derived fromthe expansive section 600B is a power source for operating compressor304. This embodiment, however, illustrates that the condenser 307 may beplaced externally from evaporator 306 and not necessarily being limitedto being placed within evaporator 306. In this situation the heat givenoff by condenser 307, including the heat of condensation, is absorbed byits environment rather than evaporator 306.

The one way heat system is not intended to be restricted for use asdescribed in this disclosure but may be useful in other applicationssuch as the use of boilers to power steam generators or applicationswhere it is desired to capture radiant energy and preclude kineticenergy from escaping.

Much of the heat utilized by the system is recycled. As previouslydiscussed, the heat recycling embodiments are summarized as follows:

1) Positioning condenser 410 within evaporator 425 causing latent heatto be given-off by condenser 410 and absorbed by the 425 evaporator.

2) Placing the condensing probe 140 deep into a tube containing theincoming seawater 152 causing heat to be absorbed by the seawater 142.

3) Utilizing a counter current heat exchange 200 for the transfer ofheat from the hot condensed water 220 emitted from the condenser 135 andcondensing probe 140 to the incoming seawater 210, such that most of theheat of the condensed water 220 is transferred to the incoming seawater210.

4) Diverting low grade heat, in the form of condensed water 220, awayfrom the counter current heat exchange 200 and delivering it into theboiler 360. The diverted low grade heat of the condensed water 220conducts heat to the liquid-phase refrigerant R410-A 351A contained inboiler 360, causing the liquid refrigerant R410-A 351A to boil in theboiler 360, thus helping to power the expander 370.

5) Utilizing a pro-warming system to warm incoming seawater from the seaby transferring heat from the condenser 380 to the seawater before itenters the holding reservoir 230.

6) Placing the piped outflow and storage containers 223 of condensedwater 220 within the intake reservoir of the seawater, allowing theresidual heat from the condensed seawater to transfer to the seawater inthe holding reservoir 230.

FIG. 7 illustrates a diagram of a distillation system with a mechanicaladvantage, wherein an expander displaces a greater volume of water vaporthan the compressor connected to the expander, according to an aspect.

In further conservation of energy, the compressive portion of the systemmay be configured such that the compressor 422-a and a second expander370-a are interconnected and transfer energy to one another. Theexpander 370-a may displace a greater volume of vapor 136 per revolutionthan the compressor 422-a does, producing a mechanical advantage system.The force exerted by the compressor 422-a and the expander 370-a may bein opposition and cancel each other out, resulting in the compressor422-a and the expander 370-a to be in equilibrium.

In this configuration a pressured chamber may be created between thecompressor 422-a and the expander 370-a, and may be referred to as aholding chamber 782. The compressor 422-a may be in fluid communicationwith the evaporator 425, and the expander 370-a may be in fluidcommunication with the condenser 410. Again, the expander 370-a maydisplace a greater volume of water vapor 136 than compressor 422-a does,creating a mechanical advantage system, wherein the pressure between theholding chamber 782 and condenser 410 is less than the pressure betweenthe holding chamber 782 and evaporator 425. Thus, the difference in thetemperature between the holding chamber 782 and condenser 410 may beless than the temperature between the holding chamber 782 and evaporator425. In this manner the water vapor 136 entering condenser 410 may be ata higher temperature than that of the seawater 211 entering evaporator425, causing a transfer of heat from condenser 410 to evaporator 425 andresulting in the seawater 211 in evaporator 425 to boil and the watervapor in condenser 410 to condense.

In order to maintain the temperature/pressure in the respectivechambers, it is important to prevent the loss of heat to avoiddisruption of the system. Hence, the respective chambers andinterconnecting components should preferably be well insulated, such as,for example, by a vacuumed encasement.

The following chart lists examples of pressure and temperature in therespective chambers:

Chart 4 Water

Holding Chamber: Temperature 112 C Pressure 22 psi (denoted by P1 andP3)

Evaporator: Temperature 89.6 C Pressure 10 psi (denoted by P2)

Condenser: Temperature 106 C Pressure 18 psi (denoted by P4)

The system in equilibrium is shown by the following equation:V1(P1−P2)=V2(P3−P4)  Equation 5:

If V2 or volume displaced by compressor 410=1 Cubic meter

Expansive Compressive(V1)(22−18) psi=1 Cubic meter)(22−10) psi.(V1)(4) psi=12 (Cubic meter) psiV1=3 Cubic meter

As an example, for the system to be at equilibrium, V1, the volume ofthe expander 370-a, must displace 3 cubic meters of volume perrevolution while V2, the volume of the compressor 422-a, must displace 1square meter of volume per revolution. In using the example pressure andtemperature parameters listed in Chart 4, the expander 370-a mustdisplace a volume of vapor greater than 3 cubic meters in order for thecompressor 422-a to be capable of compressing vapor from evaporator 425into the holding chamber 782. Additionally, a difference less than 12psi, (which corresponds to a difference in temperature of 22.4 degreesC.), between the holding chamber 782 and the evaporator 425 is requiredfor compressor 422-a to be capable of compressing vapor from evaporator425 into the holding chamber 782. The compressor 422-a and/or expander370-a may be equipped with, for example, a variable size drive pulley orother suitable means for controlling the pressure/temperature in theholding chamber 782.

It is noted that the major principles of recycling beat are generallydescribed herein and that there may exist variants or deviations thatproduce an equivalent outcome. It is the purpose of the presentinvention to encompass these variations. All embodiments may beimplemented solely or in conjunction with any combination with oneanother thereof.

As an example, when the system is at equilibrium, it is in a staticstate. The system may remain at equilibrium provided them is nodisplacement of vapor by either compressor 422-a or expander 370-a andno heat transfer from either of the chambers occur. However, in adynamic state, expander 370-a may displace a greater volume of vaporthan compressor 422-a does. Hence, compressor 422-a may be incapable ofreplenishing the volume of vapor into the holding chamber 782 inrelation to the amount that is being drawn by expander 370-a.Consequently, the holding chamber 782 may quickly lose pressure and themechanical advantage system may become disrupted.

Additionally, the density of water vapor is less at lower temperaturesthan it is at higher temperatures. As an example, if the temperature ofevaporator 425 is lower than that of the temperature of the holdingchamber 782, the density of water vapor in evaporator 425 is less thanthat of the holding chamber 782. Hence, again expander 370-a isexpelling a greater quantity of vapor from the holding chamber 782 ascompared to the amount of vapor aspirating from evaporator 425 andcompressed into the holding chamber 782. Again, the holding chamber 782loses pressure and the mechanical advantage system becomes disrupted inthis example.

FIG. 8 illustrates a diagram of a distillation system having a chemicalmechanical advantage system, according to an aspect.

To compensate for the depletion of water vapor 136 in the holdingchamber 782, additional vapor must preferably be aspirated fromevaporator 425 and compressed into the holding chamber 782. To achievethis, a first compressor 422 may be configured between the firstevaporator 425 and the holding chamber 782 and the vapor from firstevaporator 425 (“first evaporator” or “evaporator 1”) may be compressedinto the holding chamber 782. The first compressor 422 (“firstcompressor” or “compressor 1”) may be coupled to and powered by a firstexpander 370 of expansive section 800B (“expansive section,” “expansiveportion,” “expansion section,” or “expansion portion”). In this example,the expansive section 800B contains ammonia (NH₃) 883. As explainedpreviously, the expander 370 may derive its energy from the differencein pressure between the second evaporator 425-a (“second evaporator” or“evaporator 2”) and the second condenser 380, and there is an increasein pressure as the NH₃ liquid 883 boils in the second evaporator 425-aand a decrease in pressure as the NH₃ vapor 134-a condenses in thesecond condenser 380. The expansive section 800B may be fortified by,for example, solar energy applied to evaporator 425-a or replaced oraugmented by a motor to either the first compressor 422 or firstexpander 370.

Further, the vapor 136 from the first evaporator 425 must preferably becompressed and stepped up to a pressure level that reaches at least thepressure of that of the holding chamber 782. The step up mechanism maybe accomplished by the implementation of the first expander 370 ofexpansive section 800B in which expansive section 800B contains a fluidhaving different vapor pressure properties than that of water. This stepup mechanism may be referred to as a chemical mechanical advantagesystem.

As shown in FIG. 8, in the system 800, water vapor is compressed fromthe first evaporator 425 into the holding chamber 782. In this examplethe system is driven by expansion section 800B and utilizes ammonia(NH₃) 883 as its fluid. NH₃ has different vapor properties than water.The difference in vapor properties may produce a chemical typemechanical advantage.

As an example, heat for the second evaporator 425-a is provided by solarheat and is heated to 30 C and the second condenser 380 (“secondcondenser” or “condenser 2”) is cooled by sea water 210 at a temperatureof 25 C. The temperature differential between the second evaporator425-a and second condenser 380 drives the first expander 370 which inturn drives the first compressor 422, to which the first expander 370 isconnected.

Chart 5 lists the parameters for equilibrium when using H₂O in thecompressive portion 800A of the system and NH₃ in the expansive portion800B of the system.

Chart 5

Compressive Section H2O

Holding Chamber: Temperature 112 C Pressure 22 psi (denoted by P1)

Evaporator 1: Temperature 89.6 C Pressure 10 psi (denoted by P2)

Expansive Section NH3

Evaporator 2: Temperature 30 C Pressure 169.1 psi (denoted by P3)

Condenser 2: Temperature 25 C Pressure 145.5 psi (denoted by P4)

Below is the derivation for the parameters shown in chart 5 using thefollowing equation:V1(P1−P2)=V2(P3−P4)  Equation 6:

If V1 or volume displaced by compressor 1=1 cubic meter

-   -   Compressor 1 Expander 1        1 cubic meter (22−10) psi=(V2)(169.1−145.5) psi.        (12)(cubic meter) psi=(V2) 23.6 psi        0.508 (cubic meter)=V2

For the system to be at equilibrium, V2 or expander 1 must displace0.508 cubic meter of volume per revolution while V1 or compressor 1 mustdisplace 1 meter sq. of volume per revolution. In using the abovepressure and temperature parameters listed in chart 5, expander 1 mustdisplace a volume of vapor greater than 0.508 in order for compressor 1to be capable of compressing vapor from evaporator 1 into the holdingchamber.

Conversely, if V2 or volume displaced by expander 1=1 cubic meter then:V1(12) psi=(1 cubic meter) 23.6 psiV1=1.96 (cubic meter)

Compressor 1 must displace a volume of vapor less than 1.96 in order forcompressor 1 to be capable of compressing vapor from evaporator 1 intothe holding chamber.

Additionally, a difference greater than 23.6 psi, (which corresponds toa difference in temperature of 5 degrees C.), between evaporator 2 andcondenser 2 is required for compressor 1 to be capable of compressingvapor from evaporator 1 into the holding chamber. The heat differentialmay be obtained by heating evaporator 2 with a heating source such asimplementing parabolic reflectors and/or, in the condensing side,introducing a cooling source into condenser 2 in the form of piped coolseawater.

It is noted that only a difference greater than 5 degrees C. betweenevaporator 2 and condenser 2 are required to compress vapor fromcondenser 1 into the holding chamber having a difference of temperatureof 22.4 degrees C.

A pump may be necessary to pump the condensed liquid NH₃ from the lowpressure second condenser 380 to the high pressure evaporator 425-a.Regulators (984 in FIG. 9) may be placed where needed within the system.The regulators may, for example, be in the form of pumps, one way valvesor release valves in order to maintain proper pressure to make thesystem functional.

FIG. 9 illustrates a diagram of a distillation system in which excessvapor expelled from condenser 410 is directed to condenser 410-B andinto evaporator 425-a, according to an aspect.

In the previous example, the second evaporator 425-a is primarily solardriven by the expansion section 800B. However, in another example, theexcess vapor 136, not condensed by the first condenser 410, is directedinto the second evaporator 425-a. The thermal energy from the vapor 136directed from condenser 410, becomes recycled and drives or helps driveexpander 370 and in turn drives the first compressor 422

FIG. 9 depicts an example where the excess vapor that has not beencondensed in condenser 410 is delivered to condenser 410-B contained inevaporator 425-a of the expansive section 900B. Additionally, the hotwater that has been condensed in condenser 410 is also delivered tocondenser 410-B located within evaporator 425-a. The energy derived fromthe heat of the vapor or the mixture of vapor and/or condensate 136-bcauses the NH₃ 883 to boil in evaporator 425-a causing an increase inpressure in evaporator 425-a and, simultaneously, as the NH₃ vapor 136-acondenses in condenser 380, expander 370 becomes actuated. Hence, theenergy is recycled back, driving expander 370 and in turn compressor422. In this manner the energy from the excess vapor and hot condensatethat is emitted from condenser 410 is ultimately transformed and used tocompress vapor from evaporator 425 into the holding chamber 782.

Further, heat given off by condenser 380 to the incoming piped coolseawater 210 may be redirected back and preheats the seawater 210entering evaporator 425. The recycling of heat, anywhere possible, helpsin conserving energy.

The expansive system, again may be part of a step up system and mayutilize NH₃ as the second fluid. As previously discussed, the secondfluid having different vapor pressure properties than that of water,produces a chemical type mechanical advantage.

As illustrated in FIG. 9, expander 370 may be configured betweenevaporator 425-a and condenser 380 and the energy derived, from thedifference in temperature between evaporator 425-a and condenser 380, isdelivered to expander 370 and is leveraged and stepped up and in turntransferred onto compressor 422. Compressor 422 subsequently aspiratesvapor and induces boiling of the seawater in evaporator 425 andcompresses the vapor to a pressure and temperature equal to or abovethat of the holding chamber 782.

Pumps may be implemented, where needed, to regulate the length of timethe vapor/seawater 136-b are transferring heat to their respectivecomponents. The regulating pumps, in the form of pumps or releasevalves, assure that the proper temperatures and pressures within thesystem are maintained.

Chart 6 lists the parameters for equilibrium using H₂O for thecompressive portion of the system and NH₃ in the expansive portion ofthe system.

Chart 6

-   -   Compressive H2O

Holding Chamber: Temperature 112 C Pressure 22 psi (denoted by P1)

Evaporator 1: Temperature 89.6 C Pressure 10 psi (denoted by P2)

-   -   Expansive NH3

Condenser: Temperature 100 C Pressure 908.5 psi (denoted by P3)

Evaporator 1: Temperature 95 C Pressure 822.2 psi (denoted by P4)

Below is the derivation for the example parameters shown in chart 5using the following equation:

Compressive H2O Expansive NH3V1(P1−P2)=V2(P3−P4)  Equation 7:

If V1 or volume displaced by compressor 1=1 cubic meter

Thus:

-   -   Compressor 1 Expander 1        1 cubic meter. (22−10) psi=(V2)(908.5−822.2) psi.        (12) (cubic meter) psi=(V2) 86.3 psi        0.134 (cubic meter)=V2

For the system to be at equilibrium, V2 or expander 370 (expander 1)must displace 0.134 meter sq. of volume per revolution while V1 orcompressor 422 (compressor 1) must displace 1 meter sq. of volume perrevolution.

In using the above pressure and temperature parameters in the examplelisted in chart 6, expander 370 must displace a volume of vapor greaterthan 0.134 in order for compressor 422 (compressor 1) to be capable ofcompressing vapor from evaporator 425 into the holding chamber 782.

Additionally, a temperature difference greater than 86.3 psi, (whichcorresponds to a difference of in temperature of 5 degrees C.), betweenevaporator 425-a and condenser 380 is required for compressor 422 to becapable of compressing vapor from evaporator 425 into the holdingchamber 782.

The incoming seawater absorbs heat from the condensing NH₃ of condenser380 and is directed to evaporator 425. Additional external heat may beapplied as needed at any point within the system.

The outgoing condensate and the incoming seawater are subsequentlyentered into a counter current heat exchange system as previouslyillustrated in FIG. 2. Alternatively, the condensate may transfers itsresidual heat to the incoming seawater as it passes through a countercurrent latent heat exchange system (described in the next section).

The stepped up mechanism may also be achieved with the use of water asthe second fluid as opposed to NH₃. However, the stepped up mechanism inthis example is produced by conventional mechanical advantage incontrast to being produced by chemically induced mechanical advantage.The size of expander 370 would need to be increased to displace agreater volume of vapor than does compressor 422.

It should be understood that the illustrations previously discussed areonly examples and the principles shown herein may also apply to otherscenarios and applications using different fluids, mechanical ratios,temperature and pressure parameters, and so on.

FIG. 10 illustrates a diagram of a distillation system having a countercurrent heat exchange system that transfers heat through latent heat,according to an aspect.

The previously discussed counter current heat exchange system, describedwhen referring to FIG. 2, may transfer heat by conduction without theuse of latent heat. As an example, the following counter current heatexchange system transfers heat through the exchange of latent heat. Theadvantage of transferring heat through latent heat of vaporization andcondensation is that it is a much more rapid process for transferringheat as compared to the transfer of heat by general conduction. In thisexample, this is possible, in that the available heat for transfer inlatent heat of vaporization or condensation of water at 100 degrees C.is approximately 540 cal/g; thus, this provides a much more rapidprocess for transferring heat.

As an example, the hot vapor/steam and/or condensate 136-b emerging fromcondenser 410 and 410-B of FIG. 9 are passed through a thermalconductive conduit that is submerged in a liquid fluid, FIG. 10. In thisexample the liquid is NH₃ 883. However, any fluid may be used, includingwater. The heat from the steam and/or condensate 136-b conducts throughthe conduit, causing the liquid NH₃ 883 to boil and in the processabsorbs latent heat. Above the boiling NH₃ a second conduit ispositioned and transports cool seawater 210 in an opposite direction ofthat of the steam and/or condensate 136-b. As the vapor 136-a from theboiling NH₃ liquid rises it makes contact with the conduit carrying thecooler incoming seawater 210 causing the vapor 136-a to condense andfall back into the liquid NH₃ 888. As the NH₃ vapor 136-a condenses, itslatent heat is transferred to the seawater 210.

The conduit carrying the hot condensate may act in part as a boiler orevaporator and the conduit carrying the cold seawater may act as acondenser.

To make the system effective, the counter current latent heat system maybe compartmented in a series of compartments or cells. The compartmentedcells may be segmentally enclosed and each cell may contain a liquid andvapor mixture of NH₃ and a segmented portion of the conduit containingcool seawater 210 (traveling in one direction), and below a secondconduit containing hot condensate 136-b, (traveling in the oppositedirection), as the process of the NH₃ vaporizing and condensingproceeds, heat exchange may occur between the conduit carrying the hotoutgoing condensed water 136-b and the cool incoming seawater 210 asillustrated in FIG. 10. As an example, as the respective fluids withineach conduit enters each succeeding cell, the temperatures of thecondensate 136-b gradually decrease and the temperature of the seawater210 increases. At the hot and the cold ends of the system, thecondensate and the seawater should have close to the same temperature ofone another. This principle may also apply to other applications whereheat exchange from one fluid to another is desired. The hot fluid may bea vapor and or a liquid and exchange heat with a second fluid that maybe a vapor and or a liquid.

The pressures of each compartment within the series may be regulated tosupport the process of boiling and condensing of the NH₃ relative to thetemperature of the paired off incoming seawater 210 and outgoingcondensate 136-b. Preferably, the temperature and corresponding pressurewithin each of the respective compartments should be approximately theaverage of the temperature of the respective portion of the pipedoutgoing condensate 136-b and the incoming sweater 210 within theparticular compartment. Also, one-way valves 984, in both the hot andcold conduits, may be placed between each compartment, or where needed,to avoid backflow of fluid and help keep the temperatures of eachcompartment segregated. In this manner the temperature of the outgoingcondensate 136-b is hotter than the liquid NH₃ 883, (causing the liquidNH₃ to boil) and conversely the temperature of the incoming seawater 210is cooler than the NH₃ vapor 136-a, causing the NH₃ vapor 136-a tocondense and precipitate to the bottom of the compartment. If anotherfluid other than NH₃ is used, for example water, the suitable parametersof temperature and pressure within each cell must be appropriatelyadjusted.

FIG. 11 illustrates a diagram of a distillation system utilizing acombination of the stepped up system using chemical mechanical advantage(as previously described in FIG. 9), and a counter current latent heatexchange system (as previously described in FIG. 10), according to anaspect.

The advantage of combining the two systems is that first, the capabilityof leveraging and compressing the vapor from evaporator 425 into theholding chamber 782 is provided, and secondly, the use of latent heat ofvaporization and condensation provides for a much more rapid process fortransferring heat through the counter current heat exchange system.

In this example the series of evaporators (Evp 3, Evp 4, 425-a) andcondensers (380, Cond 4, Cond 3) contain NH₃. The conduit carrying thehot condensate or vapor 136-b is passed through each successivecompartment within the series of evaporators (Evp 3, Evp 4, 425-a).Conversely, the conduit carrying the cool sweater 210, (in the oppositedirection), is passed through each successive compartment within theseries of condensers (380, Cond 4, Cond 3). The conduit carrying the hotcondensate is located above the conduit carrying the cold seawater 210.Again, the hot condensate 136-b and cold seawater 210 travel in oppositedirections within their respective conduits, and, in each cell, theconduit carrying the hot condensate 136-b gives off heat and causesboiling of the NH₃ within its respective evaporators (Evp 3, Evp 4,425-a) and the conduit carrying the cold seawater 210 absorbs heat fromthe NH₃ Vapor 136-a within its respective condensers (Cond 3, Cond 4 and380). The vapor 136-a produced by (Evp 3, Evp 4, 425-a) is communicatedand condensed by condensers (Cond 3, Cond 4 and 380) respectively.Expander 370 is configured between Evp 3 and Cond 3 and may drivecompressor 422. Its energy is derived from the difference in pressure ofevaporator Evap 3 and condenser Cond 3 and may serve as a step up systemusing chemically induced mechanical advantage.

Pumps (390A, 390B, 390C) may be necessary to pump the precipitatedliquid NH₃ from each of the respective low pressure condensers (Cond 3,Cond 4, 380) to its paired high pressure evaporator in each cell.One-way valves may be placed where needed, to help keep each compartmentthermally segregated within the system. Regulators 984 may also, forexample, be in the form of pumps or release valves in order to maintainproper pressure to make the system functional.

The evaporator of any of the compartments of the system may be fortifiedby the implementation of heat, either provided by solar parabolicreflectors or other means. The illustration in FIG. 11 depicts 3compartments containing evaporators (Evp 3, Evp 4, 425-a) as well astheir respective expanders and condensers. However, the use of a greaternumber of chambers provides for a more gradual temperature gradientbetween the incoming sweater and condensate and improves the efficiencyof the system.

The series of compartmentalized evaporators (Evp 3, Evp 4, 425-a) may beencased with a vacuumed one-way heat system. As previously discussed,heat from sun rays reflected from parabolic reflectors or the likepenetrate the glass encasement, contributing heat to the series ofevaporators (Evp 3, Evp 4, 425-a) causing the NH₃ 883 refrigerant toboil. Sun rays are electromagnetic radiation carrying heat. Again, aspreviously discussed since electromagnetic waves are not impeded by avacuum, heat can be transferred through a vacuum via radiation. The heatin the evaporators becomes trapped and unable to escape to the outsideas the kinetic energy of the refrigerant molecules are unable topenetrate and pass the vacuum barrier. This configuration may become aheat trap per se.

The system may be composed of numerous cells to assure a gradually heatexchanged between the condensate 136-b to the incoming seawater 210. Inthe process heat is given off from the condensate to the incomingseawater and simultaneously the temperature of the incoming seawatergradually increases as it absorbs heat from the condensate. As therespective fluids within each conduit enters each succeeding cell, thetemperatures of the condensate 136-b gradually decrease and thetemperature of the seawater 210 increases. At the hot and the cold endsof the system, the condensate and the seawater should have close to thesame temperature of one another.

FIG. 12 illustrates a diagram of a distillation system having cells,wherein each cell contains its own evaporator, condenser and expander,in which they are configured and function similar to that described inthe segmented cell containing the paired Evp3 and Cond 3 of FIG. 11,and, also has incorporated the counter current latent heat exchangesystem (as previously discussed in FIG. 9 and FIG. 11), according to anaspect.

The expanders are depicted as 370, Exp. 1B and Exp. 1C, and may be incommunication with their respective evaporator and condenser. Each cellmay function as an independent unit. However, the expanders of each cellmay be interconnected in series and may be configured to functioncumulatively. Each expander within each cell may serve as a step upsystem using chemically induced mechanical advantage energy derived fromthe difference in pressure of its respective evaporator (425-a, Evp 2B,Evp 2C) and condenser (380, Cond 2B, Cond 2C) and the energy derivedfrom each cell is delivered to their respective expander and summedtogether and transmitted to power compressor 422. Again pumps (390A,390B, 390C) may be necessary to pump the precipitated liquid NH₃ fromthe respective low pressure condenser to the high pressure evaporator ineach cell. Regulators 984 in the form of pumps or release valves as wellas one-way valves may be used to maintain proper function of the system,and, the series of compartmentalized evaporators (425-a, Evp 2B, Evp2C), may be encased with a vacuumed one-way heat system.

This example utilizes NH₃ as the step up fluid. However, other fluidsmay be used including water. However, with each fluid, suitableparameters with regard to temperature and pressure must be appropriatelyadjusted and maintained within each cell in order for the system tofunction.

In the case of using water as opposed to NH₃, the stepped up mechanismis produced by conventional mechanical advantage in contrast to beingproduced by chemically induced mechanical advantage. The expanders inthe series of cells cumulatively sum together to displace a greatervolume of vapor than does compressor 422, resulting in a conventionalmechanical advantage, as described in FIG. 13.

FIG. 13 illustrates a diagram of a distillation system having a countercurrent latent heat exchange system using solely water, according to anaspect. This is considered when the use of NH₃ is not desired. In thisexample water itself is used.

As an example, heated brine 211 from evaporator 425 is conveyed througha series of evaporator cells (Evap 2, Evap 2B, Evap 2C). Additionally,condensate and/or steam 136-b from condenser 410, is concurrentlytransported through a conduit through the same series of evaporatorcells. The heat from the steam and condensate 136-b is absorbed by theseawater brine 211 of each evaporator cell causing the seawater brine211 to boil. The pressure and temperature within each respectiveevaporator cell is such that the brine within each cell boils. As thebrine progresses through the evaporators of each successive cell viaregulating pumps 984-a, the temperature of the brine may become lower asheat is given off to the evaporator of each cell. Simultaneously, thesalt content may become more concentrated as more and more of the brineboils off.

Concurrently, at the opposite end of the counter current latent heatexchange system, seawater 210 of lower temperature is introduced intothe series of condensers (Cond 2C, Cond 2B, 380). The seawater 210 flowsthrough a conduit and is configured to flow through the series ofcondensers in the opposite direction of the condensate 136-b that flowsthrough the series of evaporators. As the seawater progresses throughthe condenser of each successive cell, heat is absorbed from thesurrounding water vapor 136, (that has been created by the boiling ofbrine in its respective evaporator). Consequently, the temperature ofthe incoming seawater 210 progressively becomes greater. As the watervapor 136 comes in contact with the cooler piped seawater 210, itcondenses and precipitates to the button of its respective condenser andis subsequently pumped to and joins the condensate 136-b. In this mannerthe heat remaining in the precipitated water vapor is used again in thesuccessive evaporators.

Similar to the system described in FIG. 12, the expanders are depictedas 370, Exp. 1B and Exp. 1C, and may be in communication and locatedbetween their respective evaporator and condenser within the series.Each cell may function as an independent unit. Energy derived from thedifference in pressure of the boiling brine 211 of the evaporators andthe condensing of vapor 136 within the condensers in each cell, may betransferred to their respective expander. Because the expanders areinterconnected in series, the energy of the expanders (370, Exp. 1B andExp. 1C), may function cumulatively and sum together. The resultingsummation of energy in turn may be transmitted to power compressor 422.The expanders when arranged in series, cumulatively displace a greatervolume of vapor 136 than does compressor 422, resulting in aconventional mechanical advantage and stepped up mechanism.

Again pumps (390A, 390B, 390C) may be necessary to pump the precipitatedliquid from the respective low pressure condenser to the high pressureevaporator in each cell. Regulators 984 and 984-a in the form of pumpsor release valves as well as one-way valves may be used to maintainproper function of the system.

Alternatively, the energy generated by each expander within each cell,may be coupled to and transferred to a separate and designatedcompressor placed between evaporator 425 and the holding chamber 782.This configuration would result in a plurality of compressors, locatedwithin evaporator 425, being coupled to a designated expander within theseries of cells. This is in contrast to the series of evaporators beingcoupled to a single compressor located within evaporator 425.

FIG. 14 illustrates a diagram of a distillation system according to anaspect.

Similar to the distillation system depicted in FIG. 12, FIG. 14 depictsa distillation system configured having a plurality of expanders (370,Exp. 1B, Exp. 1C) interconnected and contributing energy to powercompressor 422. However, in illustration FIG. 14 compressor 422-a andexpander 370-a (depicted in FIG. 12) are eliminated such that theplurality of interconnected expanders directly power compressor 422.Many of the elements discussed in FIG. 12 as well as other elementsdiscussed in previous illustrations are not depicted here in order toavoid redundancies.

The energy provided by expanders (370, Exp. 1B, Exp. 1C) cumulativelypower compressor 422. Compressor 422 draws vapor 136 from the seawater210 contained in evaporator 425 and compresses it into condenser 410.

As previously illustrated in FIG. 12, the conduit carrying thecompressed vapor 136 and the condensate of vapor 136 is passed fromcondenser 410 through each successive compartment within the series ofevaporators (425-a, Evap. 2 b, Evap. 2 c) and as it passes through, heatis given off to each successive evaporator thus contributing heat toliquid 883 in each respective evaporator. Also, seawater 210 of lowertemperature is introduced into the series of condensers (Cond 2C, Cond2B, 380). The seawater 210 flows through a conduit 443 and is configuredto flow through the series of condensers in the opposite direction ofthe condensate 136-b that flows through the series of evaporators. Asthe seawater progresses through the condenser of each successive cell,heat is absorbed from the surrounding vapor 136-a, (that as been createdby the boiling of liquid 433 in its respective evaporator).Consequently, the temperature of the incoming seawater 210 progressivelybecomes greater. As the vapor 136-a comes in contact with the coolerpiped seawater 210, it condenses and precipitates to the button of itsrespective condenser.

Alternatively and depending on the application, conduit 446 or conduit1447 need not pass through each successive evaporator (425-a, Evap. 2 b,Evap. 2 c), in which heat is given off to liquid 883 contained in eachevaporator. Also, conduit 446 need not pass through each successivecondenser (Cond 2C, Cond 2B, 380), wherein heat is absorbed by vapor136-a in each condenser and causing vapor 136-a to condense. In thissituation, evaporator (425-a, Evap. 2 b, Evap. 2 c) may have its ownheating source. Likewise, condensers (Cond 2C, Cond 2B, 380) may haveits own cooling source.

A one-way valve 986 may be implemented, having a regulating pressurerelease mechanism, impeding the flow of vapor 136 and releasing pressureat a predetermined higher level into condenser 410. The increasedpressure level is designed to increase the temperature of vapor 136being transported by conduit 446 thru condenser 410. The increasedtemperature of vapor 136 contained in condenser 410, having a highertemperature than the seawater 210 contained in evaporator 425 causes theboiling of seawater 210.

The pressure release mechanism of one-way valve 986 regulates andcontrols the pressure and thus the temperature of vapor 136 emitted andleading into condenser 410. By monitoring the pressure of vapor 136released into condenser 410, the rate at which the seawater 410 boils isregulated.

As previously discussed, mechanical advantage is produced when thevolume of expander 370 displaces a greater volume of vapor than thatdisplaced by condenser 422. This is consistent with equation 5:

Compressive ExpansiveV1(P1−P2)=V2(P3−P4)

In this embodiment, similar principles of mechanical advantage areobserved as previously illustrated with equation 5. In thisillustration, the increased volume is achieved by using multipleinterconnected expanders. For example, expanders (370, Exp 1B, Exp. 1Care interconnected and the energy produced by each expander is summedtogether to cumulatively power condenser 422. In this situation, thevolume displaced by each expander is multiplied by the pressuredifference between the evaporator and condenser within each respectivecompartment of the series. The energy produced by each expander becomescombined to result in a cumulative force acting on compressor 422.

ThusV1(P1−P2):=V2(P3−P4)+V3(P5−P6)+V4(P7−P8) . . . etc.  equation 8:

Where: the pressure evaporators in (425-a, Evap 2B, Evap 2C) equals (P3,P5, P7) respectfully and where the pressure in condensers (380, Cond 2B,Cond 2C) equals (P4, P6, P8) respectfully and where P1 equals thepressure in evaporator 425 and P2 equals the pressure in condenser 410.

Where: V2(P3−P4) is the energy derived from the first cell of theseries.

V3 (P5−P6) is the energy derived from the second cell of the series.

V4 (P7−P8) is the energy derived from the third cell of the series.

In which V1(P1−P2) is the work done by compressor 422.

And

V2 is the volume displaced by expander 307 and (P3−P4) is the pressuredifferential acting on expander 307.

V3 is the volume displaced by expander Exp. 1B and (P8−P6) is thepressure differential acting on expander Exp. 1B.

V4 is the volume displaced by expander Exp. 1C and (P7−P8) is thepressure differential acting on expander Exp. 1C.

As previously discussed in previous embodiments, liquid 210 and liquid883 may be the same fluid. As an example, both liquid 210 and liquid 883may consist of water or both liquid 210 and liquid 883 may consist of aliquid other than water. Alternatively, liquid 210 and liquid 883 mayconsist of different fluids, having different vapor pressure properties.As an example, liquid 210 may consist of water and liquid 883 mayconsist of ammonia or vise versa liquid 210 may consist of ammonia andliquid 883 may consist of water.

Supplemental heat to fortify the system may be applied to evaporator 425or to any or all of the evaporators (425-a, Evp 2B, Exp. 2C) by anexternal heating source 411 such as electrical burners, burning naturalgas or fossil fuels or through solar energy 1412.

Additionally, solar energy 1412 may be applied to evaporators 425 andevaporators (425-a, Evp 2B, Exp. 2C). Further, evaporators 425 andevaporators (425-a, Evp 2B, Exp. 2C) may be encased with a vacuumencasement 1413 to help prevent the loss of heat to the outside of thesystem.

In the present industry, there is a serious problem controlling theformation of scale on the various components of seawater distillationsystems, particularly the scale formation on evaporators. Generally, theavoidance of scale formation requires that the seawater should not beconcentrated or boiled down to less than one third of its originalvolume.

The following embodiment, involves diminishing scaling by reducing theconcentration and build-up of salts in evaporator 425. Reducing saltconcentration may be accomplished by implementing conduit 1447 to drawout concentrated seawater 210 from evaporator 425 and replacing it withfresh and less concentrated seawater 210 delivered by conduit 443.Regulators 987 may control the flow of concentrated seawater 210 leavingevaporator 425, while regulator 984 controls the flow of fresh or lessconcentrated seawater 210 entering evaporator 425. In regulating thequantity of ingress and egress of seawater 210 in evaporator 425 thesalt content is monitored, thus avoid scaling due to high saltconcentration.

The concentrated seawater 410 drawn from evaporator 425, still containsuseful heat. The heat from the concentrated seawater 410 (or brine 1411)is recycled back into the system by transporting the brine 1411 viaconduit 1447. Conduit 1447 is submerged and passed through liquid 883contained in each evaporator (425-a Evp. 2B, Evp. 2C) of the series ofcompartments. The brine 1411, as it is transported through conduit 1447and passes through each successive evaporator, heat is given off andabsorbed by liquid 883 contained within each of the sequentialcompartments thus recycling and contributing heat to boil liquid 883.Consequently, the brine gradually becomes cooler as it passes throughthe series of compartments.

There has been great concern with regard to dumping concentrated brineinto the ocean, resulting in environmental shock and harm to theenvironment. However, an additional advantage is realized when seawater210 is drawn out of evaporator 425 before it becomes too concentrated.In doing so, the advantage is realized when expelling the high saltconcentrated brine 1411 back into the ocean is avoided.

As previously illustrated in this embodiment, recycling usable heat frombrine 1411, allows the affordability to expel brine at less concentratedlevels since much of the heat from the brine is recaptured.Traditionally, seawater is boiled down as much as possible in order todistill and extract the greatest amount of fresh water product from eachboiling cycle. This practice, results in a great amount of energy beingwasted. However, when the heat from the brine is recycled, there is lessenergy expended and the energy cost becomes less of an issue when themajor portion of the heat is recycled back into the system.

As previously discussed, a heat containment element may be incorporatedby encasing at least a portion of evaporator (425-a, Evp 28, Evp 2C)with a vacuum disposed within encasement 1413, allowing energy in theform of radiation to penetrate encasement 1413 and the vacuum layer toheat liquid 883 within each evaporator (425-a, Evp 2B, Evp 2C).Additionally, the vacuum encasement 1413 may be incorporated ontoevaporator 425 to facilitate the heating of liquid 210. The radiationenergy transforms into kinetic energy as it heats and boils liquid 883or liquid 210. The heat in the form of kinetic energy is incapable ofpenetrating and passing through the vacuum layer of the encasement 1413,thus preventing the loss of heat to the outside of the encasement thuspreserving the heat within its respective evaporator.

FIG. 15 illustrates a system similar to that depicted in FIG. 14.However, in FIG. 15 vapor 136 from evaporator 425 is compressed bycompressor 422 and is directly transported through evaporators (425-a,Evp 2B, Evp 2C). All other elements depicted in FIG. 14 may have thesame function and may be implemented in FIG. 15.

FIG. 16 illustrates an energy producing system in which theinterconnected expanders (370, Exp 1B, Exp. 1C) power generator 1622rather than powering compressor 422 of the distillation systempreviously illustrated in FIG. 14.

Alternatively, and depending on the application, expanders (370, Exp118, Exp. 1C) may power compressor 422, such as the compressorillustrated in FIG. 14. For the purpose of simplification, thecompressor is not shown in FIG. 15.

Similar to the expansive section previously illustrated in FIG. 12 andFIG. 14, FIG. 15 depicts the series of expanders (370, Exp 1B, Exp. 1C)being interconnected. The individual expanders are in communication andlocated between their respective evaporator and condenser. Each cell mayfunction as an independent unit with each expander of the seriescontributing energy to power generator 1622.

Again as previously discussed, the energy acting upon each expander isderived from the difference in pressure produced by the boiling liquid883 in each evaporator and its paired condenser, wherein vapor 833condenses into a liquid. Because the expanders are interconnected inseries, the energy of the expanders (370, Exp 1B, Exp. 1C), may functioncumulatively and summed together. The resulting summation of the energyin turn may be transmitted to power generator 1622 or compressor 422.

In the instance in which expanders (370, Exp 1B, Exp. 1C), powers acompressor, the expanders when arranged in series, cumulativelydisplaces a greater volume of vapor 833-a than does the compressor,resulting in a mechanical advantage mechanism.

Again, pumps (390A, 390B, 390C) may be necessary to pump theprecipitated liquid 883 from the low-pressure condenser to the highpressure evaporator in each cell.

The energy source may be derived from solar radiation. The solar energy1412 may be in the form of solar radiation collected and concentratedwith the use of reflective mirrors and directed to evaporator (425-a,Evp 2B, Evp 2C) to boil liquid 883. The resultant vapor 833-a arisingfrom the boiling of liquid 833 causes an increase pressure in eachrespective evaporator which in turn exerts pressure on its pairedexpander.

A cooling source 1611 such as water or air, absorbs heat from condensers(380, Cond 2B, Cond 2C) causing vapor 833-a to condense resulting in lowpressure in each condenser of the series.

As previously discussed, each expander in the series of compartments ispowered by the difference in pressure between its respective evaporatorand condenser and in turn the energy derived from each expander aresummed together and transmitted to power generator 1622.

Again, as previously discussed, a heat containment element may beincorporated by encasing at least a portion of evaporator (425-a, Evp2B, Evp 2C) with a vacuum disposed within encasement 1413, allowingenergy in the form of radiation to penetrate encasement 1413 and thevacuum layer to heat liquid 883. The heat in the form of kinetic energyis incapable of penetrating and passing through the vacuum layer ofencasement 1413, thus preventing the loss of heat to the outside ofencasement 1413 and its respective evaporator.

It should be understood that the major principles of recycling heat amgenerally described herein and that there may exist variants ordeviations that produce an equivalent outcome. It is the purpose of thisdisclosure to encompass these variations.

All embodiments described herein may be used solely or in anycombination with one another as well as in partial form. Also, it shouldbe understood that the use of, for example, pumps, one way valves orrelease valves, vacuumed one-way heat system, and so on, are utilizedwhere needed, and in some descriptions are not mentioned in order tosimplify the descriptions and avoid being redundant.

Although specific embodiments have been illustrated and described hereinfor the purpose of disclosing the preferred embodiments, someone ofordinary skills in the art will easily detect alternate embodimentsand/or equivalent variations, which may be capable of achieving the sameresults, and which may be substituted for the specific embodimentsillustrated and described herein without departing from the scope of theinvention. Therefore, the scope of this application is intended to coveralternate embodiments and/or equivalent variations of the specificembodiments illustrated and/or described herein. Hence, the scope of theinvention is defined by the accompanying claims and their equivalents.Furthermore, each and every claim is incorporated as further disclosureinto the specification and the claims are embodiment(s) of theinvention.

What is claimed is:
 1. An energy recycling system comprising: a firstevaporator containing in a first portion a first liquid having a firsttemperature which is at the first liquid's boiling point; a firstconduit in which a first vapor of the first liquid received from thefirst evaporator is compressed by a compressor, thus causing the firstvapor in the first conduit to have a second temperature, higher than thefirst temperature; a first expander configured to drive the compressorto compress the first vapor from the first evaporator into the firstconduit, the first conduit having thermo-conductive properties andfunctioning as a first condenser, wherein the second temperature of thefirst vapor in the first conduit having a higher temperature than thefirst temperature, causing a heat transfer from the first vapor in thefirst conduit to the first liquid, and thus the boiling of the firstliquid, when the first conduit passes through the first evaporator;wherein the first conduit containing a first fluid comprised of at leastone member of the group consisting of the first vapor and a condensateof the first vapor passes through a second evaporator, at least aportion of the first vapor within the first conduit condenses into thecondensate of the first vapor, and, wherein the first expander driven bya second vapor of a second fluid expands the second vapor contained bythe second evaporator into a second condenser the second liquid having athird temperature which is at the second liquid's boiling point but islower than the second temperature, such that boiling of the secondliquid occurs, generating the second vapor, when the first conduit ispassed from the first evaporator and passes through the secondevaporator; wherein the third temperature is greater than a fourthtemperature of the second vapor in the second condenser, furthercomprising a second conduit, having thermo-conductive properties,transporting the first liquid, having a fifth temperature lower than thefourth temperature, to the first evaporator after passing through thesecond condenser and absorbing therein heat from the second vapor,causing condensation of the second vapor, further a pump is provided forpumping the second liquid from the second condenser to the secondevaporator.
 2. The energy recycling system of claim 1, wherein amechanical advantage is applied between the first expander and thecompressor, the mechanical advantage is achieved by at least one of thegroup consisting of the first expander displacing a greater volume ofvapor than the compressor and the first expander displacing vapor havingdifferent vapor pressure properties than that displaced by thecompressor.
 3. The energy recycling system of claim 1, wherein thesecond conduit is passed through at least one additional condenserbefore reaching the second condenser and the first evaporator, so thatthe first liquid absorbs heat also from the at least one additionalcondenser, the at least one additional condenser and the secondcondenser forming a series of condensers leading to the firstevaporator, with gradually increasing temperatures, and, wherein thefirst conduit, leaving the first evaporator and into the secondevaporator passes through at least one additional evaporator, so thatthe first fluid loses heat also to the at least one additionalevaporator, the second evaporator and the at least one additionalevaporator forming a series of evaporators with gradually decreasingtemperatures, wherein the second vapor of each evaporator contained inthe at least one additional evaporator is in fluid communication with apaired condenser of the at least one additional condenser; the secondvapor condenses into the second liquid when the second vapor comes incontact with the second conduit containing the first liquid.
 4. Theenergy recycling system of claim 3, wherein the at least one additionalevaporator is a plurality of evaporators and the at least one additionalcondenser is a plurality of condenser, wherein the first conduit passesthrough the plurality of evaporators and the second conduit passingthrough the plurality of condensers, the plurality of evaporators andthe plurality of condensers creating a series of evaporators and aseries of condensers, the second liquid in each of the plurality ofevaporates having gradually decreasing boiling points from a first endof the series to an opposite second end, such that the boiling point ofthe second liquid in each of the plurality of evaporators is lower thanthe corresponding second temperature and higher than the correspondingfifth temperature, as the first fluid travels through the first conduitfrom the first end to the second end of the series of evaporators andhaving gradually increasing temperatures in the plurality of condensersas the first liquid travels through the second conduit from the secondend to the first end of the series of condensers.
 5. The energyrecycling system of claim 3, wherein between each air of the at leastone additional evaporator and the at least one additional condenser anadditional expander is placed and used to help drive the compressor,further providing an additional pump to pump the second liquid from theat least one additional condenser to the at least one additionalevaporator.
 6. The energy recycling system of claim 5, wherein theenergy derived from each additional expander are summed together andtransmitted to power the compressor.
 7. The distillation system of claim5, wherein the compressor is powered by at least one of the groupconsisting of a motor, the expander and each additional expander.
 8. Theenergy recycling system of claim 3, wherein at least an evaporativeportion of the system is insulated using a vacuum encasement.
 9. Theenergy recycling system of claim 3, in a heat containment application,wherein at least one of the group consisting of the second evaporatorand the at least one additional evaporator containing the second liquidand, comprises an encasing, and a vacuum disposed within the encasing,and the encasing allows energy in the form of radiation to penetrate theencasing and the vacuum layer, and the radiation energy transforms intokinetic energy as the radiation heats and boils the second liquidcontained in the at least one of the group consisting of the secondevaporator and the at least one additional evaporator, further the heatin the form of kinetic energy is incapable of penetrating and passingthrough the vacuum layer, thus preventing the loss of heat to theoutside of the encasing of the at least one of the group consisting ofthe first evaporator, the second evaporator and the at least oneadditional evaporator resulting in greater energy efficiency to drivethe expander.
 10. The energy recycling system of claim 3, wherein athird conduit, having thermal conductive properties, transporting thefirst liquid from the first evaporator, having the first temperature,through the second evaporator, and, passing, through at least oneadditional evaporator, so that the first liquid loses heat to the secondevaporator and to the at least one additional evaporator, the secondevaporator and the at least one additional evaporator forming a seriesof evaporators with gradually decreasing temperatures.
 11. The energyrecycling system of claim 1, wherein the first liquid is water and thesecond liquid is at least one of the group consisting of water and aliquid other than water.
 12. The energy recycling system of claim 1,wherein a heat exchange system comprising at least one closedcompartment containing in a first portion the second liquid having thethird temperature which is at the second liquid's boiling point; thefirst conduit, after passing through the first evaporator, containing afirst fluid comprised of at least one of the group consisting of thefirst vapor and the condensate of the first vapor having the secondtemperature which is higher than the third temperature and submerged inthe second liquid, causing the second liquid to absorb heat from thesecond temperature and at least a portion of the second liquid to boilwithin the first portion of the at least one closed compartment, andthus convert to the second vapor; and, transporting the first liquid tothe first evaporator from a second portion of the at least one closedcompartment and having the fifth temperature, which is lower than thethird temperature, and passing through the second portion of the atleast one closed compartment where the second vapors, come in contactwith the second conduit containing the first liquid having the fifthtemperature, causing the second vapors to lose heat and condense, andthus join the second liquid in the second portion of the at least oneclosed compartment; further comprising an additional pump for thedelivery of the second liquid from the second portion to the firstportion of the at least one closed compartment.
 13. The energy recyclingsystem of claim of claim 12, wherein the system comprises a plurality ofclosed compartments, which are adjacent to each other, each closedcompartment having a pressure and thus corresponding third temperatureand boiling point, such that to create a series of closed compartmentshaving a gradually changing third temperature and corresponding boilingpoint of the second liquid from a first end of the series to an oppositesecond end, as the first fluid travels through the first conduit fromthe first end to the second end of the series and the first liquidtravels through the second conduit from the second end to the first endof the series, where the third temperature in each closed compartment islower than the corresponding second temperature and higher than thefifth temperature.
 14. The energy recycling system of claim 13, whereina system to drive the compressor consists of a second expander coupledto the compressor, the second expander configured between the firstportion and the second portion of the at least one closed compartment;and the second portion having a fourth temperature lower than the firstportion having the third temperature, and the second expander powered bythe temperature and corresponding pressure difference between the firstportion and second portion of the at least one closed compartment. 15.The energy recycling system of claim 14, wherein a mechanical advantageis applied between the second expander and the compressor, themechanical advantage is achieved by at least one of the group consistingof the second expander displacing a greater volume of vapor than thecompressor and the second expander displacing vapor having differentvapor pressure properties than that displaced by the compressor.
 16. Theenergy recycling system of claim 14, wherein the energy derived fromeach second expander of the at least one closed compartment are summedtogether and transmitted to power the compressor.
 17. A distillationsystem comprising: a first evaporator containing in a first portion afirst liquid having a first temperature which is at the first liquid'sboiling point; a first conduit in which a first vapor of the firstliquid received from the first evaporator is compressed by a compressor,thus causing the first vapor in the first conduit to have a secondtemperature, higher than the first temperature; a first expanderconfigured to drive the compressor to compress the first vapor from thefirst evaporator into the first conduit and through a second evaporator,the first conduit having thermo-conductive properties and functioning asa first condenser, wherein the second temperature of the first vapor inthe first conduit having a higher temperature than a third temperaturein the second evaporator, causing a heat transfer from the first vaporin the first conduit to a second liquid contained in the secondevaporator, and thus the boiling of the second liquid, when the firstconduit passes through the second evaporator; wherein the first conduitcontaining a first fluid comprised of at least one member of the groupconsisting of the first vapor and a condensate of the first vapor passesthrough the second evaporator, at least a portion of the first vaporwithin the first conduit condenses into the condensate of the firstvapor, and, wherein the first expander driven by a second vapor of thesecond liquid expands the second vapor contained by the secondevaporator into a second condenser, the second liquid having the thirdtemperature which is at the second liquid's boiling point but is lowerthan the second temperature, such that boiling of the second liquidoccurs, generating the second vapor, when the first conduit is passedfrom the first evaporator and passes through the second evaporator;wherein the third temperature is greater than a fourth temperature ofthe second vapor in the second condenser, further comprising a secondconduit, having thermo-conductive properties, transporting the firstliquid, having a fifth temperature lower than the fourth temperature, tothe first evaporator after passing through the second condenser andabsorbing therein heat from the second vapor, causing condensation ofthe second vapor, further a pump is provided for pumping the secondliquid from the second condenser to the second evaporator.
 18. Thedistillation system of claim 17, wherein the second conduit is passedthrough at least one additional condenser before reaching the secondcondenser and first evaporator, so that the first liquid absorbs heatalso from the at least one additional condenser, the second condenserand the at least one additional condenser forming a series ofcondensers, leading to the first evaporator, with gradually increasingtemperatures, and, wherein the first conduit, leaving the firstevaporator and into the second evaporator, and, passes through at leastone additional evaporator, so that the first fluid loses heat also tothe at least one additional evaporator, the second evaporator and the atleast one additional evaporator forming a series of evaporators withgradually decreasing temperatures, wherein the second vapor of eachevaporator contained in the at least one additional evaporator is influid communication with a paired condenser of the at least oneadditional condenser; the second vapor condenses into the second liquidwhen the second vapor comes in contact with the second conduitcontaining the first liquid.
 19. The distillation system of claim 18,wherein between each pair of the at least one additional evaporator andthe at least one additional condenser an additional expander is placedand used to help drive the compressor, further providing an additionalpump to pump the second liquid from the at least one additionalcondenser to the at least one additional evaporator.
 20. Thedistillation system of claim 17, wherein the compressor is powered by amotor.